US5430181A - Process for improving a controlled oxidation reaction - Google Patents

Process for improving a controlled oxidation reaction Download PDF

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US5430181A
US5430181A US08/019,878 US1987893A US5430181A US 5430181 A US5430181 A US 5430181A US 1987893 A US1987893 A US 1987893A US 5430181 A US5430181 A US 5430181A
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oxidation
give
additional gas
oxygen
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Philippe Arpentinier
Jacques Koenig
Yves Torre
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LAir Liquide SA pour lEtude et lExploitation des Procedes Georges Claude
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LAir Liquide SA pour lEtude et lExploitation des Procedes Georges Claude
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    • C—CHEMISTRY; METALLURGY
    • C07—ORGANIC CHEMISTRY
    • C07D—HETEROCYCLIC COMPOUNDS
    • C07D301/00—Preparation of oxiranes
    • C07D301/02—Synthesis of the oxirane ring
    • C07D301/03—Synthesis of the oxirane ring by oxidation of unsaturated compounds, or of mixtures of unsaturated and saturated compounds
    • C07D301/19—Synthesis of the oxirane ring by oxidation of unsaturated compounds, or of mixtures of unsaturated and saturated compounds with organic hydroperoxides
    • C—CHEMISTRY; METALLURGY
    • C07—ORGANIC CHEMISTRY
    • C07B—GENERAL METHODS OF ORGANIC CHEMISTRY; APPARATUS THEREFOR
    • C07B33/00—Oxidation in general
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    • C07B41/00—Formation or introduction of functional groups containing oxygen
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    • C07C—ACYCLIC OR CARBOCYCLIC COMPOUNDS
    • C07C17/00—Preparation of halogenated hydrocarbons
    • C07C17/093—Preparation of halogenated hydrocarbons by replacement by halogens
    • C07C17/15—Preparation of halogenated hydrocarbons by replacement by halogens with oxygen as auxiliary reagent, e.g. oxychlorination
    • C07C17/152—Preparation of halogenated hydrocarbons by replacement by halogens with oxygen as auxiliary reagent, e.g. oxychlorination of hydrocarbons
    • C07C17/156—Preparation of halogenated hydrocarbons by replacement by halogens with oxygen as auxiliary reagent, e.g. oxychlorination of hydrocarbons of unsaturated hydrocarbons
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    • C07—ORGANIC CHEMISTRY
    • C07C—ACYCLIC OR CARBOCYCLIC COMPOUNDS
    • C07C37/00—Preparation of compounds having hydroxy or O-metal groups bound to a carbon atom of a six-membered aromatic ring
    • C07C37/50—Preparation of compounds having hydroxy or O-metal groups bound to a carbon atom of a six-membered aromatic ring by reactions decreasing the number of carbon atoms
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    • C07C—ACYCLIC OR CARBOCYCLIC COMPOUNDS
    • C07C37/00—Preparation of compounds having hydroxy or O-metal groups bound to a carbon atom of a six-membered aromatic ring
    • C07C37/58—Preparation of compounds having hydroxy or O-metal groups bound to a carbon atom of a six-membered aromatic ring by oxidation reactions introducing directly hydroxy groups on a =CH-group belonging to a six-membered aromatic ring with the aid of molecular oxygen
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    • C07—ORGANIC CHEMISTRY
    • C07C—ACYCLIC OR CARBOCYCLIC COMPOUNDS
    • C07C45/00—Preparation of compounds having >C = O groups bound only to carbon or hydrogen atoms; Preparation of chelates of such compounds
    • C07C45/27—Preparation of compounds having >C = O groups bound only to carbon or hydrogen atoms; Preparation of chelates of such compounds by oxidation
    • C07C45/32—Preparation of compounds having >C = O groups bound only to carbon or hydrogen atoms; Preparation of chelates of such compounds by oxidation with molecular oxygen
    • C07C45/33—Preparation of compounds having >C = O groups bound only to carbon or hydrogen atoms; Preparation of chelates of such compounds by oxidation with molecular oxygen of CHx-moieties
    • C07C45/34—Preparation of compounds having >C = O groups bound only to carbon or hydrogen atoms; Preparation of chelates of such compounds by oxidation with molecular oxygen of CHx-moieties in unsaturated compounds
    • C—CHEMISTRY; METALLURGY
    • C07—ORGANIC CHEMISTRY
    • C07C—ACYCLIC OR CARBOCYCLIC COMPOUNDS
    • C07C45/00—Preparation of compounds having >C = O groups bound only to carbon or hydrogen atoms; Preparation of chelates of such compounds
    • C07C45/27—Preparation of compounds having >C = O groups bound only to carbon or hydrogen atoms; Preparation of chelates of such compounds by oxidation
    • C07C45/32—Preparation of compounds having >C = O groups bound only to carbon or hydrogen atoms; Preparation of chelates of such compounds by oxidation with molecular oxygen
    • C07C45/37—Preparation of compounds having >C = O groups bound only to carbon or hydrogen atoms; Preparation of chelates of such compounds by oxidation with molecular oxygen of >C—O—functional groups to >C=O groups
    • C07C45/38—Preparation of compounds having >C = O groups bound only to carbon or hydrogen atoms; Preparation of chelates of such compounds by oxidation with molecular oxygen of >C—O—functional groups to >C=O groups being a primary hydroxyl group
    • C—CHEMISTRY; METALLURGY
    • C07—ORGANIC CHEMISTRY
    • C07C—ACYCLIC OR CARBOCYCLIC COMPOUNDS
    • C07C45/00—Preparation of compounds having >C = O groups bound only to carbon or hydrogen atoms; Preparation of chelates of such compounds
    • C07C45/27—Preparation of compounds having >C = O groups bound only to carbon or hydrogen atoms; Preparation of chelates of such compounds by oxidation
    • C07C45/32—Preparation of compounds having >C = O groups bound only to carbon or hydrogen atoms; Preparation of chelates of such compounds by oxidation with molecular oxygen
    • C07C45/37—Preparation of compounds having >C = O groups bound only to carbon or hydrogen atoms; Preparation of chelates of such compounds by oxidation with molecular oxygen of >C—O—functional groups to >C=O groups
    • C07C45/39—Preparation of compounds having >C = O groups bound only to carbon or hydrogen atoms; Preparation of chelates of such compounds by oxidation with molecular oxygen of >C—O—functional groups to >C=O groups being a secondary hydroxyl group
    • C—CHEMISTRY; METALLURGY
    • C07—ORGANIC CHEMISTRY
    • C07C—ACYCLIC OR CARBOCYCLIC COMPOUNDS
    • C07C51/00—Preparation of carboxylic acids or their salts, halides or anhydrides
    • C07C51/16—Preparation of carboxylic acids or their salts, halides or anhydrides by oxidation
    • C07C51/21—Preparation of carboxylic acids or their salts, halides or anhydrides by oxidation with molecular oxygen
    • C07C51/215—Preparation of carboxylic acids or their salts, halides or anhydrides by oxidation with molecular oxygen of saturated hydrocarbyl groups
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    • C07—ORGANIC CHEMISTRY
    • C07C—ACYCLIC OR CARBOCYCLIC COMPOUNDS
    • C07C51/00—Preparation of carboxylic acids or their salts, halides or anhydrides
    • C07C51/16—Preparation of carboxylic acids or their salts, halides or anhydrides by oxidation
    • C07C51/21—Preparation of carboxylic acids or their salts, halides or anhydrides by oxidation with molecular oxygen
    • C07C51/23—Preparation of carboxylic acids or their salts, halides or anhydrides by oxidation with molecular oxygen of oxygen-containing groups to carboxyl groups
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    • C07—ORGANIC CHEMISTRY
    • C07C—ACYCLIC OR CARBOCYCLIC COMPOUNDS
    • C07C51/00—Preparation of carboxylic acids or their salts, halides or anhydrides
    • C07C51/16—Preparation of carboxylic acids or their salts, halides or anhydrides by oxidation
    • C07C51/21—Preparation of carboxylic acids or their salts, halides or anhydrides by oxidation with molecular oxygen
    • C07C51/23—Preparation of carboxylic acids or their salts, halides or anhydrides by oxidation with molecular oxygen of oxygen-containing groups to carboxyl groups
    • C07C51/235—Preparation of carboxylic acids or their salts, halides or anhydrides by oxidation with molecular oxygen of oxygen-containing groups to carboxyl groups of —CHO groups or primary alcohol groups
    • C—CHEMISTRY; METALLURGY
    • C07—ORGANIC CHEMISTRY
    • C07C—ACYCLIC OR CARBOCYCLIC COMPOUNDS
    • C07C51/00—Preparation of carboxylic acids or their salts, halides or anhydrides
    • C07C51/16—Preparation of carboxylic acids or their salts, halides or anhydrides by oxidation
    • C07C51/21—Preparation of carboxylic acids or their salts, halides or anhydrides by oxidation with molecular oxygen
    • C07C51/25—Preparation of carboxylic acids or their salts, halides or anhydrides by oxidation with molecular oxygen of unsaturated compounds containing no six-membered aromatic ring
    • C07C51/252—Preparation of carboxylic acids or their salts, halides or anhydrides by oxidation with molecular oxygen of unsaturated compounds containing no six-membered aromatic ring of propene, butenes, acrolein or methacrolein
    • C—CHEMISTRY; METALLURGY
    • C07—ORGANIC CHEMISTRY
    • C07C—ACYCLIC OR CARBOCYCLIC COMPOUNDS
    • C07C51/00—Preparation of carboxylic acids or their salts, halides or anhydrides
    • C07C51/16—Preparation of carboxylic acids or their salts, halides or anhydrides by oxidation
    • C07C51/21—Preparation of carboxylic acids or their salts, halides or anhydrides by oxidation with molecular oxygen
    • C07C51/255—Preparation of carboxylic acids or their salts, halides or anhydrides by oxidation with molecular oxygen of compounds containing six-membered aromatic rings without ring-splitting
    • C07C51/265—Preparation of carboxylic acids or their salts, halides or anhydrides by oxidation with molecular oxygen of compounds containing six-membered aromatic rings without ring-splitting having alkyl side chains which are oxidised to carboxyl groups
    • C—CHEMISTRY; METALLURGY
    • C07—ORGANIC CHEMISTRY
    • C07C—ACYCLIC OR CARBOCYCLIC COMPOUNDS
    • C07C51/00—Preparation of carboxylic acids or their salts, halides or anhydrides
    • C07C51/16—Preparation of carboxylic acids or their salts, halides or anhydrides by oxidation
    • C07C51/31—Preparation of carboxylic acids or their salts, halides or anhydrides by oxidation of cyclic compounds with ring-splitting
    • C07C51/313—Preparation of carboxylic acids or their salts, halides or anhydrides by oxidation of cyclic compounds with ring-splitting with molecular oxygen
    • C—CHEMISTRY; METALLURGY
    • C07—ORGANIC CHEMISTRY
    • C07C—ACYCLIC OR CARBOCYCLIC COMPOUNDS
    • C07C67/00—Preparation of carboxylic acid esters
    • C07C67/04—Preparation of carboxylic acid esters by reacting carboxylic acids or symmetrical anhydrides onto unsaturated carbon-to-carbon bonds
    • C07C67/05—Preparation of carboxylic acid esters by reacting carboxylic acids or symmetrical anhydrides onto unsaturated carbon-to-carbon bonds with oxidation
    • C—CHEMISTRY; METALLURGY
    • C07—ORGANIC CHEMISTRY
    • C07C—ACYCLIC OR CARBOCYCLIC COMPOUNDS
    • C07C67/00—Preparation of carboxylic acid esters
    • C07C67/39—Preparation of carboxylic acid esters by oxidation of groups which are precursors for the acid moiety of the ester
    • Y—GENERAL TAGGING OF NEW TECHNOLOGICAL DEVELOPMENTS; GENERAL TAGGING OF CROSS-SECTIONAL TECHNOLOGIES SPANNING OVER SEVERAL SECTIONS OF THE IPC; TECHNICAL SUBJECTS COVERED BY FORMER USPC CROSS-REFERENCE ART COLLECTIONS [XRACs] AND DIGESTS
    • Y02—TECHNOLOGIES OR APPLICATIONS FOR MITIGATION OR ADAPTATION AGAINST CLIMATE CHANGE
    • Y02P—CLIMATE CHANGE MITIGATION TECHNOLOGIES IN THE PRODUCTION OR PROCESSING OF GOODS
    • Y02P20/00—Technologies relating to chemical industry
    • Y02P20/50—Improvements relating to the production of bulk chemicals
    • Y02P20/52—Improvements relating to the production of bulk chemicals using catalysts, e.g. selective catalysts

Definitions

  • the present invention concerns a process for improving the selectivity of a controlled oxidation reaction between at least one reactant and oxygen in order to give a final product for improving either the capacity or the yield of a production unit where this controlled oxidation reaction is carried out.
  • Controlled oxidation reaction (I) is the one leading to the intended product and it is the one that should consequently be preferred as compared to the other reactions.
  • reaction (II) consisting in the total oxidation of the reactants into CO 2 and H 2 O, is clearly more exothermic than main reaction (I).
  • This type of oxidation reactions under industrial conditions, usually rely on air as a source of oxygen, the nitrogen from the air being inert towards the reactants used.
  • the selectivity of the process in terms of intended product is generally low as compared to the maximum theoretical selectivity. This relatively low selectivity is examined by the strong contribution of the secondary reactions, in particular reaction (II), with the corresponding release of heat, which causes technical problems in removing this heat and limits the yield of conversion for each pass.
  • the selectivity of the intended product and the conversion yield may be improved by increasing the concentration of oxygen in the reaction mixture.
  • This concentration is limited either by technical problems of evacuation of the reaction heat or by the range of inflammability of the mixture at the inlet or the outlet of the reactor as well as at any other point of the reactive section.
  • any mixture of combustible reactant and oxygen may ignite when its oxygen content exceeds a certain maximum value, which is inherent to each reaction mixture and to the pressure and temperature conditions used. In the conditions of use of this type of reaction, it is therefore suitable not to exceed this maximum value of oxygen which is permissible at any point of the reactive section of a production unit where the oxidation reaction is used and in particular in the reaction mixture, for example for safety reasons.
  • German patent 1,254,137 describes a process for the manufacture of ethylene oxide by oxidation of ethylene, in which methane is introduced into the reaction mixture in order to increase the concentration of oxygen in the reaction zone.
  • this German patent strictly only concerns the oxidation of ethylene in the presence of methane in order to give ethylene oxide. It is particularly noticeable that ethane is considered within the framework of this oxidation reaction, as having an effect which is contrary to that of methane.
  • German patent has not solved one of the problems raised above, namely, increasing the concentration of permissible oxygen in a reaction mixture in order to increase the productivity of any controlled oxidation reaction other than the oxidation of an alkene to give an alkene oxide.
  • the present invention therefore concerns a process enabling to improve the selectivity of a controlled oxidation reaction.
  • a second object of the invention consists in enabling to increase the concentration of permissible oxygen in the reaction mixture and this, without any problem of safety.
  • a third object of the invention consists in providing a reaction mixture in which the thermic properties for example heat conductivity and specific heat, are improved, thereby permitting a better control of the temperature of the oxidation reaction, as well as an easier removal of the reaction heat at the level of the reactor.
  • Another object of the invention consists in improving the capacity or yield of a production unit in the operation of a controlled oxidation reaction.
  • the present invention therefore concerns a process for improving a controlled oxidation reaction between at least one reactant and oxygen or a gas containing oxygen, which constitute a reaction mixture, characterized in that at least one reactant is reacted with oxygen in the presence of at least an additional gas which is introduced in said reaction mixture and is selected from methane, ethane, and helium, and, possibly, the product resulting from the oxidation reaction is treated in order to give a final product, the oxidation reaction of an alkene by means of oxygen in order to give an alkene oxide being excluded.
  • FIG. 1 represents the ternary diagram of the reaction mixture used in the process of oxidizing propylene in order to give acrylic acid in the presence of different additional gases or nitrogen;
  • FIG. 2 represents the ternary diagram of the reaction mixture used in the process of oxidizing n-butane in order to give maleic anhydride in the presence of different additional gases or nitrogen.
  • the molar content of the additional gas which is introduced into the reaction mixture, which consists of the reactant(s) and oxygen used is between 5 and 80%, preferably between 10 and 70% and more generally between 20 and 60%.
  • the oxygen used in the controlled oxidation reaction may be pure oxygen or a gas containing oxygen and a gas which is inert towards said controlled oxidation reaction.
  • reaction mixture may include one or more inert gases such as nitrogen.
  • an additional gas introduced into the reaction mixture means that said additional gas is effectively introduced into the constituted reaction mixture, and also that the additional gas may be previously mixed with oxygen or with the oxygen containing gas, or, preferably with the reactant(s), which will form the reaction mixture.
  • the additional gas may also result from a controlled oxidation reaction previously used according to the process of the invention, and which is recycled for a new operation, possibly after treatment and/or separation, by adsorption and/or absorption, and/or distillation, and/or fractionated condensation and/or permeation.
  • a controlled oxidation reaction previously used according to the process of the invention, and which is recycled for a new operation, possibly after treatment and/or separation, by adsorption and/or absorption, and/or distillation, and/or fractionated condensation and/or permeation.
  • methane or ethane as additional inert gas for a controlled oxidation reaction, these gases being normally well known for their property to ignite.
  • methane and, in a lesser extent ethane are preferred additional gases for increasing the concentration of oxygen in the reaction mixture, and this still more importantly than helium or carbon dioxide which are reputed to be inert.
  • curves 1, 2, 3 and 4 correspond, respectively, to the use of nitrogen, carbon dioxide, ethane and methane as additional gases.
  • the operation is repeated many times with variable contents of reactant, so as to permit a plurality of points to be obtained on the ternary diagram.
  • the process according to the invention enables to use a permissible content of oxygen in the reaction mixture which be higher by 1 to 40% molar, more generally 1 to 20% molar (% absolute in the reaction mixture), than the permissible oxygen content when an additional gas according to the invention is not introduced into said reaction mixture.
  • the oxidation reactions according to the process of the invention may be carried out under atmospheric pressure, but also at a pressure higher than 0.1 MPa, preferably at a pressure between 0.2 and 5 MPa, more preferably between 0.2 and 1.5 MPa.
  • the additional gases according to the invention may also, through their heat conductivity and their specific heat be used to improve greatly the heat conductivity and the global specific heat of the reaction mixture, which facilitates the removal of heat for the same quantity of product being treated.
  • Another object of the invention consists in utilizing at least one additional gas selected from methane, ethane, carbon dioxide and helium in order to improve the removal of reaction heat produced during a controlled oxidation reaction, the oxidation reaction of an alkene by means of oxygen in order to give an alkene oxide being excluded.
  • the additional gas is preferably helium or methane.
  • an additional gas according to the invention for example in order to improve the removal of reaction heat, is more particularly adapted to oxidation reactions carried out on a fixed bed.
  • the process according to the invention may be used to improve any controlled oxidation reaction, whether it be carried out in a gas phase or in a gas-liquid phase.
  • Variable contents of propylene and additional gases or nitrogen are introduced into a stainless steel container which is provided with an igniting device.
  • the mixtures thus obtained are homogenized and increasing contents of oxygen are introduced therein until the mixture ignites.
  • the conditions of pressure and temperature are those normally used in the industry to carry out this controlled oxidation reaction.
  • Example I The procedure of Example I is repeated in order to determine the maximum permissible oxygen content in a mixture consisting of n-butane and oxygen, which is used on an industrial basis to produce maleic anhydride.
  • the conditions of pressure and temperature are those normally used in the industry to carry out this controlled oxidation reaction.
  • Oxychlorination of ethylene in air in a fixed bed Oxychlorination of ethylene in air in a fixed bed.
  • This reaction is carried out in three reactors disposed in series and operating in a fixed bed.
  • Each reactor includes as catalyst, copper and potassium chlorides supported on balls of alumina of 3 mm diameter.
  • the first reactor is supplied with the following compounds:
  • the oxygen introduced into the first reactor represents 80% of the total oxygen used in the process.
  • the oxychlorination reaction is carried out in each of three reactors at an average temperature of 214° C. and at a pressure of 6.25 bar absolute.
  • the product mixture resulting from the reaction of oxychlorination from the first reactor is sent into the second reactor, which is supplied with 12% of the total oxygen used, then in the third reactor supplied by the remaining 8% of the oxygen used.

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Abstract

Process for improving a controlled oxidation reaction between at least one reactant and oxygen, in which at least one reactant is reacted with oxygen or an oxygen containing gas, constituting a reaction mixture, in the presence of at least one additional gas which is introduced into said reaction mixture and is selected from methane, ethane and helium, and the resulting reaction product from the oxidation reaction is possibly treated so as to give a final product.

Description

BACKGROUND OF INVENTION
1. Field of the Invention
The present invention concerns a process for improving the selectivity of a controlled oxidation reaction between at least one reactant and oxygen in order to give a final product for improving either the capacity or the yield of a production unit where this controlled oxidation reaction is carried out.
2. Description of Prior Art
Most of the oxidation reactions which are used in the chemical industry are based on the following scheme:
(I) REACTANT(S)+O2 →PRODUCT(S) Controlled oxidation
(II) REACTANT(S)+O2 →CO2 +H2 O Complete oxidation
(III) REACTANT(S)+O2 →CO2 +H2 O
(IV REACTANTS+O2 →COPRODUCTS Secondary reactions
(V) COPRODUCTS+O2 →CO2 +H2 O
Controlled oxidation reaction (I) is the one leading to the intended product and it is the one that should consequently be preferred as compared to the other reactions.
Reactions (I) and (II) are generally predominant, the others often being clearly less important.
It should be noted that reaction (II) consisting in the total oxidation of the reactants into CO2 and H2 O, is clearly more exothermic than main reaction (I).
This type of oxidation reactions, under industrial conditions, usually rely on air as a source of oxygen, the nitrogen from the air being inert towards the reactants used.
The selectivity of the process in terms of intended product is generally low as compared to the maximum theoretical selectivity. This relatively low selectivity is examined by the strong contribution of the secondary reactions, in particular reaction (II), with the corresponding release of heat, which causes technical problems in removing this heat and limits the yield of conversion for each pass.
For a large majority of the processes of oxidation, the selectivity of the intended product and the conversion yield may be improved by increasing the concentration of oxygen in the reaction mixture. This concentration is limited either by technical problems of evacuation of the reaction heat or by the range of inflammability of the mixture at the inlet or the outlet of the reactor as well as at any other point of the reactive section. As a matter of fact, any mixture of combustible reactant and oxygen may ignite when its oxygen content exceeds a certain maximum value, which is inherent to each reaction mixture and to the pressure and temperature conditions used. In the conditions of use of this type of reaction, it is therefore suitable not to exceed this maximum value of oxygen which is permissible at any point of the reactive section of a production unit where the oxidation reaction is used and in particular in the reaction mixture, for example for safety reasons.
It would still be particularly interesting, for a mixture of the same reactant and oxygen, under similar conditions of pressure and temperatures, to improve the removal of the reaction heat and to increase the concentration of oxygen which is permissible in the reaction mixture without for this reason only, of course, igniting it.
German patent 1,254,137 describes a process for the manufacture of ethylene oxide by oxidation of ethylene, in which methane is introduced into the reaction mixture in order to increase the concentration of oxygen in the reaction zone. However, this German patent strictly only concerns the oxidation of ethylene in the presence of methane in order to give ethylene oxide. It is particularly noticeable that ethane is considered within the framework of this oxidation reaction, as having an effect which is contrary to that of methane.
On the other hand, it is indicated in this same German patent that until then, it was considered essential that the concentration of paraffin hydrocarbons in the circuit, and consequently also in the ethylene feed, be reduced to a minimum.
This enables to explain why, since 1962, no other oxidation reaction, except the one described in said German patent, was used in the presence of methane or another paraffin hydrocarbon.
As a matter of fact, if it can be considered that within the framework of the oxidation of alkene, essentially ethylene, in order to give an alkene oxide such as ethylene oxide, methane, contrary to ethane, enables to increase the permissible concentration of oxygen, one skilled in the art would have no reason, in view of said German patent, to use a paraffin hydrocarbon, known to be detrimental in view of its tendency to ignite, in order to increase the concentration of oxygen in another oxidation reaction. In other words, it appears, according to the teaching of this German patent, that the use of methane in order to increase the permissible concentration of oxygen is recommended only in the case of the oxidation of an alkene, such as ethylene, in order to give an alkene oxide, such as ethylene oxide.
The German patent has not solved one of the problems raised above, namely, increasing the concentration of permissible oxygen in a reaction mixture in order to increase the productivity of any controlled oxidation reaction other than the oxidation of an alkene to give an alkene oxide.
The present invention therefore concerns a process enabling to improve the selectivity of a controlled oxidation reaction. A second object of the invention consists in enabling to increase the concentration of permissible oxygen in the reaction mixture and this, without any problem of safety.
A third object of the invention consists in providing a reaction mixture in which the thermic properties for example heat conductivity and specific heat, are improved, thereby permitting a better control of the temperature of the oxidation reaction, as well as an easier removal of the reaction heat at the level of the reactor.
Another object of the invention consists in improving the capacity or yield of a production unit in the operation of a controlled oxidation reaction.
SUMMARY OF INVENTION
The present invention therefore concerns a process for improving a controlled oxidation reaction between at least one reactant and oxygen or a gas containing oxygen, which constitute a reaction mixture, characterized in that at least one reactant is reacted with oxygen in the presence of at least an additional gas which is introduced in said reaction mixture and is selected from methane, ethane, and helium, and, possibly, the product resulting from the oxidation reaction is treated in order to give a final product, the oxidation reaction of an alkene by means of oxygen in order to give an alkene oxide being excluded.
BRIEF DESCRIPTION OF DRAWINGS
Other characteristics and advantages of the present invention will now be described with reference to the annexed drawings in which:
FIG. 1 represents the ternary diagram of the reaction mixture used in the process of oxidizing propylene in order to give acrylic acid in the presence of different additional gases or nitrogen; and
FIG. 2 represents the ternary diagram of the reaction mixture used in the process of oxidizing n-butane in order to give maleic anhydride in the presence of different additional gases or nitrogen.
DESCRIPTION OF PREFERRED EMBODIMENT
Usually, the molar content of the additional gas which is introduced into the reaction mixture, which consists of the reactant(s) and oxygen used, is between 5 and 80%, preferably between 10 and 70% and more generally between 20 and 60%.
The oxygen used in the controlled oxidation reaction, according to the process of the invention, may be pure oxygen or a gas containing oxygen and a gas which is inert towards said controlled oxidation reaction.
Such a gas containing oxygen is more often air or oxygen enriched air. It will then be understood that in addition to the additional gas according to the invention, the reaction mixture may include one or more inert gases such as nitrogen.
According to the present invention, the expression "an additional gas introduced into the reaction mixture" means that said additional gas is effectively introduced into the constituted reaction mixture, and also that the additional gas may be previously mixed with oxygen or with the oxygen containing gas, or, preferably with the reactant(s), which will form the reaction mixture.
The additional gas may also result from a controlled oxidation reaction previously used according to the process of the invention, and which is recycled for a new operation, possibly after treatment and/or separation, by adsorption and/or absorption, and/or distillation, and/or fractionated condensation and/or permeation. The unexpected aspect that constitutes the use of such gases is mentioned again here, particularly, methane or ethane as additional inert gas for a controlled oxidation reaction, these gases being normally well known for their property to ignite. This is also more surprising because, within the scope of the present invention, methane and, in a lesser extent ethane, are preferred additional gases for increasing the concentration of oxygen in the reaction mixture, and this still more importantly than helium or carbon dioxide which are reputed to be inert.
It is one of the merits of the present invention to have relied on such properties of these gases in other controlled oxidation reactions than those of the oxidation of an alkene with oxygen of methane to give an alkene oxide, since this type of reaction, up to now, has been considered as a specific case which could not be adapted to other controlled oxidation reactions.
This possibility of improving controlled oxidation reactions by utilizing an additional inert gas has been proposed as a result of experimental data, on the basis of which ternary diagrams of controlled oxidation reactions which were carried out in the presence of different additional gases and under conditions of pressure and temperature normally used for this type of reaction, have been plotted. It could thus be observed that notwithstanding the nature of the controlled oxidation reaction, the permissible content of oxygen in the reaction mixture is always increased when an additional gas selected from methane, ethane, helium or carbon dioxide is used as compared to another gas, normally nitrogen. FIGS. 1 and 2 show these results in the frame work respectively, of the oxidation of propylene in order to produce acrylic acid and the oxidation of n-butane in order to produce maleic anhydride, carried out under normal conditions of temperatures and pressure. For each of these figures, curves 1, 2, 3 and 4 correspond, respectively, to the use of nitrogen, carbon dioxide, ethane and methane as additional gases.
The plots of these curves have been obtained experimentally according to the method known per se described hereinafter.
In a stainless steel container, provided with an igniting device, predetermined contents of the reactant(s) and of the additional gas have been introduced. These compounds were homogenized by means of a stirring device.
Increasing contents of oxygen are then introduced into the container until the reaction mixture explodes. The oxygen content at which the explosion takes place is indicated on a diagram, as a function of the content of the reactant used.
The operation is repeated many times with variable contents of reactant, so as to permit a plurality of points to be obtained on the ternary diagram.
Depending on the nature of the oxidation reaction, the process according to the invention enables to use a permissible content of oxygen in the reaction mixture which be higher by 1 to 40% molar, more generally 1 to 20% molar (% absolute in the reaction mixture), than the permissible oxygen content when an additional gas according to the invention is not introduced into said reaction mixture.
The oxidation reactions according to the process of the invention may be carried out under atmospheric pressure, but also at a pressure higher than 0.1 MPa, preferably at a pressure between 0.2 and 5 MPa, more preferably between 0.2 and 1.5 MPa.
In addition to their interest in increasing the concentration of permissible oxygen in the reaction mixture which is utilized, the additional gases according to the invention, may also, through their heat conductivity and their specific heat be used to improve greatly the heat conductivity and the global specific heat of the reaction mixture, which facilitates the removal of heat for the same quantity of product being treated.
To the extend that the heat removal from the reaction mixture is improved, it is then possible to increase either the capacity or the yield of a production unit which is used in carrying out a controlled oxidation reaction. Another object of the invention then consists in utilizing at least one additional gas selected from methane, ethane, carbon dioxide and helium in order to improve the removal of reaction heat produced during a controlled oxidation reaction, the oxidation reaction of an alkene by means of oxygen in order to give an alkene oxide being excluded.
In order to carry out the process according to the invention, more particularly for improving the heat conductivity and the global specific heat of the reaction mixture, the additional gas is preferably helium or methane.
The use of an additional gas according to the invention, for example in order to improve the removal of reaction heat, is more particularly adapted to oxidation reactions carried out on a fixed bed.
The process according to the invention may be used to improve any controlled oxidation reaction, whether it be carried out in a gas phase or in a gas-liquid phase.
The process according to the invention in particularly adapted to the following controlled oxidation reactions:
oxidation of cumene to prepare phenol;
oxychlorination of ethylene into dichloroethane;
oxychlorination of benzene to prepare phenol;
oxidation of toluene to prepare benzoic acid or phenol;
oxidation of isobutane or ethylbenzene to give propylene oxide;
oxidation of ethylene in liqud phase to give acetaldehyde;
oxidation of acetaldehyde, n-butane, light oils (mostly in C5 -C6) or n-butenes to give acidic acid;
oxidation of propylene or isopropanol to give acetone;
oxidation of ethylene in the presence of acetic acid to give vinyl acetate;
oxidation of butadiene inithe presence of acetic acid to give butanediol-1,4;
oxidation of propylene to give acrylic acid;
oxidation of tertiary butyl alcohol in order to give methacrylic acid;
oxidation of cyclohexane to give caprolactam and adipic acid;
oxidation of p-xylene, toluene or p-toluene aldehyde to give terephthalic acid;
oxidation of p-xylene to give dimethyl terephthalate;
oxidation of benzene, n-butenes or n-butane to give maleic anhydride;
oxidation of orthoxylene or naphthalene to give phthalic anhydride;
oxidation of methanol to give formaldehyde;
oxidation of glyoxal to give glycol; oxidation of an aldehyde to give carboxylic anhydrides or acids.
The following examples intend to illustrate the invention:
EXAMPLE 1
In order to determine the maximum permissible content of oxygen in a mixture consisting of propylene and oxygen, and used on an industrial basis to produce acrylic acid, the following procedure is followed:
Variable contents of propylene and additional gases or nitrogen are introduced into a stainless steel container which is provided with an igniting device. The mixtures thus obtained are homogenized and increasing contents of oxygen are introduced therein until the mixture ignites.
The conditions of pressure and temperature are those normally used in the industry to carry out this controlled oxidation reaction.
The maximum permissible content of oxygen, beyond which the mixture ignites is given in Table I which follows.
______________________________________                                    
                    Additional    Nature of                               
Propylene  Oxygen   gas or nitrogen                                       
                                  additional                              
(% mol.)   (% mol.) (% mol.)      gas                                     
______________________________________                                    
6.8        15       78.2          nitrogen                                
15.5       22       62.5                                                  
6.6        18       75.4          CO.sub.2                                
15.3       24       60.7                                                  
8          40.3     51.7          methane                                 
28         41       31                                                    
4          29       67            ethane                                  
13.6       32       54.4                                                  
______________________________________
From Table I, it clearly appears clearly that the oxygen content in the mixture is substantially increased when an additional gas according to the invention is introduced as compared to the permissible oxygen content when only nitrogen is introduced into the mixture.
EXAMPLE 2
The procedure of Example I is repeated in order to determine the maximum permissible oxygen content in a mixture consisting of n-butane and oxygen, which is used on an industrial basis to produce maleic anhydride.
The conditions of pressure and temperature are those normally used in the industry to carry out this controlled oxidation reaction.
The maximum permissible oxygen content beyond which the mixture ignites is given in Table II which follows:
______________________________________                                    
                   additional gas                                         
n-butane  oxygen   or nitrogen  nature of                                 
(% mol.)  (% mol.) (% mol.)     additional gas                            
______________________________________                                    
2.15      13       84.85        nitrogen                                  
4.3       14       82.70                                                  
8.3       17       74.70                                                  
4.15      17       78.85        CO.sub.2                                  
8.1       19       72.90                                                  
5         41       54           methane                                   
10        41.8     48.20                                                  
5         30       75           ethane                                    
10        32       58                                                     
______________________________________
These results as well as those obtained in Example I, show that the introduction of methane, ethane or carbon dioxide in a mixture enables to substantially increase the maximum permissible content of oxygen.
EXAMPLE 3
Oxychlorination of ethylene in air in a fixed bed.
This reaction is carried out in three reactors disposed in series and operating in a fixed bed. Each reactor includes as catalyst, copper and potassium chlorides supported on balls of alumina of 3 mm diameter.
The first reactor is supplied with the following compounds:
______________________________________                                    
               % mol.                                                     
______________________________________                                    
nitrogen         30                                                       
oxygen           8.8                                                      
ethylene         21                                                       
hydrochloric acid                                                         
                 36.9                                                     
helium           3.3                                                      
______________________________________
The oxygen introduced into the first reactor represents 80% of the total oxygen used in the process.
The oxychlorination reaction is carried out in each of three reactors at an average temperature of 214° C. and at a pressure of 6.25 bar absolute.
The product mixture resulting from the reaction of oxychlorination from the first reactor is sent into the second reactor, which is supplied with 12% of the total oxygen used, then in the third reactor supplied by the remaining 8% of the oxygen used.
At the outlet of the third reactor, a flow of 443 kilomoles/h of dichloroethane is recovered.
By way of comparison, an oxychlorination reaction is carried out under the same conditions as above, but where helium has been replaced with nitrogen. At the outlet of the third reactor, a flow of 432 kilomoles/h dichloroethane is recovered.
It is therefore observed that the use of helium enables to increase the treatment capacity of the unit by 2.5% which is substantial on an industrial basis. This increase is due to the fact that helium permits a better heat removal from the reaction mixture. Thus, a 30° C. decrease of the temperature of the hot zone was noted in the first reactor when helium was used instead of nitrogen.

Claims (23)

We claim:
1. Process for improving by increasing the permissible oxygen concentration in a controlled oxidation reaction between at least one reactant and oxygen, wherein at least one reactant is reacted with at least one member of the group consisting of oxygen and oxygen containing gases, to produce a reaction mixture, in the presence of at least one additional gas different from said at least one reactant which is introduced into said reaction mixture wherein said additional gas comprises at least one member selected from the group consisting of methane and ethane, and wherein the mole content of said additional gas in said reaction mixture is between 3.3 and 80% the oxidation reaction of an alkene by means of oxygen to give an alkene oxide being excluded.
2. Process according to claim 1, wherein the mole content of the additional gas in the reaction mixture is between 5 and 80%.
3. Process according to claim 1, wherein the oxidation is carried out at a pressure which is at least 0.1 MPa.
4. Process according to claim 1, wherein the additional gas is methane or a mixture of methane and any one of ethane, carbon dioxide and helium or a mixture thereof.
5. Process according to claim 1, wherein the permissible content of oxygen in the reaction mixture is higher by 1 to 40% molar, (% absolute in the reaction mixture), than the permissible oxygen content in a same reaction mixture in which no said additional gas has been introduced.
6. Process according to claim 1, wherein the additional gas is pre-mixed with said oxygen.
7. Process according to claim 1, wherein the additional gas introduced into the reaction mixture is obtained from a controlled oxidation reaction carried out according to the process of claim 1.
8. Process according to claim 7, wherein the reaction is carried out after said additional gas is subjected to a separation operation.
9. Process according to claim 1, wherein the controlled oxidation reaction is selected from the group consisting of:
oxidation of cumene to prepare phenol;
oxychlorination of ethylene into dichloroethane;
oxychlorination of benzene to prepare phenol;
oxidation of toluene to prepare benzoic acid;
oxidation of toluene to prepare phenol;
oxidation of isobutane or ethylbenzene to give propylene oxide;
oxidation of ethylene in liquid phase to give acetaldehyde;
oxidation of acetaldehyde to give acetic acid;
oxidation of n-butane to give acetic acid;
oxidation of light oils to give acetic acid;
oxidation of n-butenes to give acetic acid;
oxidation of propylene to give acetone;
oxidation of isopropanol to give acetone;
oxidation of ethylene in the presence of acetic acid to give vinyl acetate;
oxidation of butadiene in the presence of acetic acid to give butanediol-1,4;
oxidation of propylene to give acrylic acid;
oxidation of tertiary butyl alcohol to give methacrylic acid;
oxidation of cyclohexane to give caprolactam and adipic acid;
oxidation of p-xylene to give terephthalic acid;
oxidation of toluene to give terephthalic acid;
oxidation of p-toluene aldehyde to give terephthalic acid;
oxidation of p-xylene to give dimethyl terephthalate;
oxidation of benzene to give maleic anhydride;
oxidation of n-butenes to give maleic anhydride;
oxidation of n-butane to give maleic anhydride;
oxidation of orthoxylene to give phthalic anhydride;
oxidation of naphthalene to give phthalic anhydride;
oxidation of methanol to give formaldehyde;
oxidation of glyoxal to give glycol;
oxidation of an aldehyde to give carboxylic anhydrides; and
oxidation of an aldehyde to give carboxylic acids.
10. Method which comprises using at least one additional gas selected from the group consisting of methane, ethane and carbon dioxide to increase the permissible oxygen content in a controlled oxidation reaction, wherein said oxygen content in said reaction is 1 to 40 mole % greater than the permissible oxygen content in a reaction not containing said additional gas, wherein the mole content of the additional gas in the reaction mixture is between 3.3 and 80% and wherein said at least one additional gas is different from a reactant gas, the oxidation reaction of an alkene by means of oxygen to give an alkene oxide being excluded.
11. Method according to claim 10, wherein said additional gas is methane.
12. Process according to claim 1, wherein a product resulting from the oxidation reaction is treated to give a final product.
13. Process according to claim 1, wherein the molar content of the additional gas in the reaction mixture is between 10 and 70%.
14. Process according to claim 1, wherein the molar content of the additional gas in the reaction mixture is between 20 and 60%.
15. Process according to claim 1, wherein the oxidation is carried out at a pressure which is between 0.2 and 5 Mpa.
16. Process according to claim 1, wherein the oxidation is carried out at a pressure which is between 0.2 and 1.5 Mpa.
17. Process according to claim 1, wherein the content of oxygen in the reaction mixture is higher by 1 to 20% molar (% absolute in the reaction mixture) than the oxygen content in a same reaction mixture in which no said additional gas has been introduced.
18. Process according to claim 1, wherein the additional gas is pre-mixed with said oxygen containing gas.
19. Process according to claim 1, wherein the additional gas is pre-mixed with said at least one reactant.
20. Process according to claim 8, wherein said separation operation is at least one member selected from the group consisting of adsorption, absorption, distillation, fractionated condensation and permeation.
21. Method according to claim 10, wherein said additional gas is a mixture of methane and any one of ethane, carbon dioxide and helium.
22. Process according to claim 1, wherein the additional gas is ethane or a mixture of ethane and any one of methane, carbon dioxide and helium or a mixture thereof.
23. Method according to claim 10, wherein said additional gas is ethane or a mixture of ethane and any one of methane, carbon dioxide and helium or a mixture thereof.
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US6194588B1 (en) 1998-02-18 2001-02-27 Nippon Shokubai Co., Ltd. Method for production of maleic anhydride
US6215027B1 (en) 1998-10-20 2001-04-10 Praxair Technology, Inc. Ballast gas use in liquid phase oxidation
CN108025998A (en) * 2015-09-18 2018-05-11 国际壳牌研究有限公司 Alkanes oxidative dehydrogenation
US11319265B2 (en) 2018-11-02 2022-05-03 Shell Usa, Inc. Separation of ethane oxidative dehydrogenation effluent

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FR2903688B1 (en) * 2006-07-13 2008-09-05 Arkema France PROCESS FOR THE SYNTHESIS OF FORMALDEHYDE BY OXIDATION OF METHANOL IN THE PRESENCE OF METHANE
FR2903689B1 (en) * 2006-07-13 2008-09-05 Arkema France PROCESS FOR THE SYNTHESIS OF LIGHT ALDEHYDE BY CATALYTIC OXIDATION OF THE CORRESPONDING ALCOHOL IN THE PRESENCE OF METHANE
EP2695875A1 (en) * 2012-08-09 2014-02-12 Linde Aktiengesellschaft Improved method for the oxidation of alkyl aromatic hydrocarbons

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US6194588B1 (en) 1998-02-18 2001-02-27 Nippon Shokubai Co., Ltd. Method for production of maleic anhydride
US6215027B1 (en) 1998-10-20 2001-04-10 Praxair Technology, Inc. Ballast gas use in liquid phase oxidation
CN108025998A (en) * 2015-09-18 2018-05-11 国际壳牌研究有限公司 Alkanes oxidative dehydrogenation
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ES2099919T3 (en) 1997-06-01
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